Reforming using platinum agglomerated iridium catalysts

ABSTRACT

A method for reforming naphtha feeds which comprises contacting said feed, in the presence of hydrogen and at reforming conditions, with a catalyst comprised of platinum and iridium agglomerated to exhibit a crystallinity of at least 50% as measured by X-ray, and an alumina support material modified with at least about 100 wppm of Si and at least 10 wppm and one or more alkaline earth metals selected from Ca, Mg, Ba, and Sr, wherein the total amount of modifier does not exceed about 5000 wppm.

FIELD OF THE INVENTION

The present invention relates to process for reforming naphthas usingnovel platinum agglomerated iridium alumina catalysts containing amodifier comprised of at least about 100 wppm of Si and at least 10 wppmof one or more alkaline earth metals selected from Ca, Mg, Ba, and Sr,wherein the total amount of modifier does not exceed about 5000 wppm.

BACKGROUND OF THE INVENTION

Catalytic reforming, or hydroforming, is a well established industrialprocess employed by the petroleum industry for improving the octanequality of naphthas and straight run gasolines. In fact, it is theprimary source of octane in the modern refinery. Reforming can bedefined as the total effect of the molecular changes, or hydrocarbonreactions, produced by dehydrogenation of cyclohexanes anddehydroisomerization of alkylcyclopentanes to yield aromatics;isomerization of n-paraffins; isomerization of alkylcycloparaffins toyield cyclohexanes; isomerization of substituted aromatics; andhydrocracking of paraffins which produces gas, and inevitably coke, thelatter being deposited on the catalyst. In catalytic reforming, amulti-functional catalyst is employed which contains a metalhydrogenationdehydrogenation (hydrogen transfer) component, orcomponents, usually platinum, substantially atomically dispersed uponthe surface of a porous, inorganic oxide support, such as alumina. Thealumina support, which usually contains a halide, particularly chloride,provides the acid functionality needed for isomerization, cyclization,and hydrocracking reactions.

Reforming reactions are both endothermic and exothermic, the formerbeing predominant, particularly in the early stages of reforming withthe latter being predominant in the latter stages. In view thereof, ithas become the practice to employ a reforming unit comprised of aplurality of serially connected reactors with provision for heating ofthe reaction stream from one reactor to another. There are three majortypes of reforming: semiregenerative, cyclic, and continuous. Fixed-bedreactors are usually employed in semiregenerative and cyclic reformingand moving-bed reactors in continuous reforming. In semiregenerativereforming, the entire reforming process unit is operated by graduallyand progressively increasing the temperature to compensate fordeactivation of the catalyst caused by coke deposition, until finallythe entire unit is shut-down for regeneration and reactivation of thecatalyst. In cyclic reforming, the reactors are individually isolated,or in effect swung out of line, by various piping arrangements. Thecatalyst is regenerated by removing coke deposits, and then reactivatedwhile the other reactors of the series remain on stream. The "swingreactor" temporarily replaces a reactor which is removed from the seriesfor regeneration and reactivation of the catalyst, which is then putback in the series. In continuous reforming, the reactors are moving-bedreactors, as opposed to fixed-bed reactors, with continuous addition andwithdrawal of catalyst, and the catalyst is regenerated in a separateregeneration vessel.

In an era of limited and expensive feedstocks, the demand for additionalaromatics (octane) must be satisfied while maximizing both liquid andaromatic yields. For this reason, catalysts offering higher selectivityto liquid products will replace those of lower selectivity. Activityremains an equally important catalytic parameter and must be retained ata level equal to, or ideally greater than, that of current commercialtechnology. It is recognized in the art that one of the keys toselectivity control is the suppression of cracking reactions occurringover both the metal and acid sites of bifunctional reforming catalysts.Acid cracking reactions lead primarily to propane and isobutane and tohigher isoparaffins, which are more difficult to aromatize and hencemore prone to both metal and acid site cracking. While a certain levelof catalyst acidity is required to initiate certain essentialisomerization reactions, overly active acidity leads to both yield lossand deactivation. Specific steps to moderate, or control, acid crackingreactions in catalytic reforming are not common in the art. Eliminationof these cracking reactions is desirable for two reasons: first thelight C₁ -C₄ gases produced are of lesser value than reformate; andsecond, activity and liquid yield are tied to the retention andaromatization of feed paraffins.

Sulfur is sometimes used to modify reforming catalyst selectivity byprincipally suppressing methane formation. While sulfur is effective forthis purpose, its use introduces process complications, which could beavoided if catalyst sulfiding were not essential. Furthermore, certainnon-reforming active metals have been shown to decrease metal sitecracking reactions, principally of the internal type yielding C₃ and C₄hydrocarbons. Examples of such metals include copper, gold, silver, andtin. Since these metals are normally used in conjunction with sulfur, auniversal decline in all light gas products results.

While much work has been done over the years in developing improvedreforming catalysts, it has generally focused on such things asconcentration and combination of catalytically active metals, and typeand pore size distribution of the support material. Other work hasresulted in the modification of support materials by introducing acatalytically effective amount of an alkali or alkaline earth metalcomposite into the support. See for example, U.S. Pat. Nos. 2,602,771;2,930,763 and 3,714,281.

Although commercially, successful catalysts have resulted from suchwork, there still exists a need in the art for further improvement,especially with regard to both catalyst activity and selectivity. Inaccordance with the present invention, a new approach is describedwherein reformate yield is improved with simultaneous suppression ofboth metal and acid site cracking through the use of a novel supportmaterial which universally decreases all cracking reactions. Whilecatalyst activity, as measured by conversion, decreases as a consequenceof decreased cracking, aromatization activity and aromatics selectivityessential to catalytic reforming are retained and improved. Furthermore,the support materials of the present invention permit catalystssupported on the material to be operated in an unsulfided state.

SUMMARY OF THE INVENTION

In accordance with the present invention, there is provided a processfor reforming a naphtha feed, which process comprises contacting saidfeed, in the presence of hydrogen and at reforming conditions, with aplatinum-iridium on modified-alumina reforming catalyst, wherein theiridium component is agglomerated and exhibits a crystallinity greaterthan about 50%, as measured by x-ray diffraction, which catalysts arecomprised of: about 0.01 to 2 wt. % Pt; about 0.01 to 2 wt. % Ir; up toabout 2 wt. % of rhenium; up to about 2 wt. % tin; up to about 3.5 wt. %of a halide; and the balance being a modified alumina support modifiedwith at least about 100 wppm Si and at least 10 wppm of one or morealkaline-earth metals selected from Ca, Mg, Ba, and Sr, wherein thetotal amount of modifier does not exceed about 5000 wppm.

In a preferred embodiment of the present invention, the iridium exhibitsa crystallinity greater than about 75%, and about 0.1 to 0.7 of each ofplatinum and iridium, and about 0.5 to 1.5 wt. % chloride, are present.

In other preferred embodiments of the present invention, another metal,preferably Re, is present in an amount ranging from about 0.01 to 2 wt.%.

In another preferred embodiment of the present invention, the alumina isgamma alumina.

In yet other preferred embodiments of the present invention, themodifier is comprised of about 100 to 200 wppm of Si and about 100 to3000 wppm of an alkaline earth metal selected from Mg and Ca, and thecrystallinity of the agglomerated iridium is substantially 100%.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 is plot of data of Table II hereof which shows activity as afunction of time for heptane reforming of Catalysts F, O, N, and P.

FIG. 2 is a plot of data of Table II hereof showing yield as a functionof time also for Catalysts F, O, N, and P.

DETAILED DESCRIPTION OF THE INVENTION

Aluminas suitable for modification in accordance with the presentinvention are any of the high purity aluminas suitable for use as asupport for reforming catalysts. The term, high purity alumina, means analumina which is at least 99% pure, preferably at least 99.5% pure, andmore preferably at least 99.9% pure. The alumina can be synthetic ornaturally occurring, although synthetic alumina is preferred because itspreparation can be controlled to insure the appropriate level of purityand desired physical characteristics. It is also preferred that thealumina be one which upon calcination forms gamma alumina. By "analumina which upon calcination forms gamma alumina" it is meant analumina which is essentially in the trihydrate form prior tocalcination, and which upon calcination is, according to the crystalpattern, gamma alumina. Principally, these aluminas are derived fromprecipitation methods or, preferably, the digestion of metallic aluminumby a weak organic acid.

In a preferred precipitation method, the alumina is prepared by theaddition of an acid or acid salt such as hydrochloric acid or any of thealums to an alkali metal aluminate, such as sodium or potassiumaluminate.

The most preferred aluminas suitable for use herein are those preparedby digesting, or reacting, metallic aluminum with a weak organic acid toform an alumina sol. Preferred weak organic acids include acetic andformic acid. It is also preferred that the aluminum be digested in thepresence of a mercury compound, such as a mercury aluminum hydroxidecomplex of acetic acid. Such processes are well known to those skilledin the art and are described in U.S. Pat. Nos. 2,274,634; Re 22,196 and2,859,183; all of which are incorporated herein by reference. Aspreviously mentioned, in such a process, an alpha aluminum salt isprepared by dissolving metallic aluminum in a dilute (about 1-6 wt. %)organic acid in the presence of a mercury compound. The aluminum andmercury form an amalgam which slowly dissolves with the evolution ofhydrogen to alumina salt containing mercury, undissolved aluminum, andother materials. If desired, the resulting sol can be treated with asufficient amount of ammonium hydroxide to obtain a pH of about 6.8 to7.8, to form a gel which can be dried and calcined. It is preferred thatthe sol not be gelled, but that it be sprayed-dried to produce a highpurity alumina hydrate powder, which can then be ground to anappropriate particle size. Although not critical for the practice of thepresent invention, an appropriate particle size is from about 5 to 15microns.

The modified aluminas of the present invention are prepared byincorporating therein an effective amount of modifier. The modifier issuch that when used in an effective amount it contributes to theresulting reforming catalyst having improved overall selectivity withrespect to liquid yield with simultaneous suppression of both metal andacid site cracking, when compared to a similar catalyst not containingsuch modifiers. By the term "effective amount of modifier" is meant thatconcentration range of modifier which will improve the selectivity andreduce the cracking tendencies of the resulting catalysts when used inreforming. Generally, the modifier of the catalysts of the presentinvention is comprised of at least about 100 wppm Si and at least about10 wppm of one or more alkaline earth metals selected from Ca, Mg, Ba,and Sr, wherein the total amount of modifier does not exceed about 5000wppm. Preferred is about 100 to 200 wppm Si and about 100 to 3000 wppmalkaline earth metal. More preferred is about 100 to 200 wppm Si and 200to 1000 wppm of an alkaline earth metal selected from Ca and Mg. Mostpreferred is when the alkaline earth metal is Mg.

As previously mentioned herein, the modifiers of this invention arecomprised of Si plus one or more alkaline earth metals selected from Ca,Mg, Ba, and Sr. Preferred is Si with Ca, Mg, or both, particularly thehalides, nitrates, nitrites, oxides, hydroxides, and carbonates. It ispreferred that Si be introduced as a compound of Si which will form astable aqueous solution, or stable emulsion, in aqueous media. Organicderivatives of Si and Si-polymers, such as silicon oils, are examples ofpreferred Si compounds.

The modifier component can be incorporated into the alumina during anystage of alumina hydrate, alumina, or catalyst production. In aparticularly preferred production scheme for producing the modifiedalumina of this invention, high purity alumina hydrate powder is firstprepared by digesting metallic aluminum in a weak organic acid, therebyforming an alumina sol which is then spray-dried by a conventionalspray-drying technique to produce the alumina hydrate powder. If thealumina hydrate powder is not of appropriate particle size, it can beground by any conventional grinding means for reducing the particle sizeof refractory powders. The alumina hydrate powder is then blended withan effective amount of water, or sol, to form a paste of sufficientconsistency for extrusion. The alumina paste is then extruded into anappropriate shape, such as pellets, dried and calcined at temperaturesfrom about 400° C. to about 650° C. Active metals can then beimpregnated into the alumina by conventional impregnation means to formthe reforming catalyst. Non-limiting examples of suitable active metalsinclude platinum, rhenium, iridium, tin, copper, and mixtures thereof.It is understood that modern reforming catalysts universally includeplatinum as one of the active metals, with or without one or more otheractive metals.

The modifier component can be introduced in any one or more of the aboveprocess steps. For example, during preparation of the alumina powder,the modifier component, in the form of a water soluble salt, can beblended with the alumina sol prior to spray-drying. It can also beblended with the alumina hydrate powder, which blend can then be furtherblended with the alumina sol to form the extrusion paste. Further, thealumina hydrate powder and alumina sol can first be blended whereuponthe modifier component can be added with sufficient water to form anextrudable paste. It is also understood that the modifier component canbe mixed with the alumina powder prior to grinding. Although themodifier component can concurrently be incorporated into the aluminahydrate material after extrusion by conventional impregnationtechniques, it is preferred to introduce the modifier component prior toextrusion to ensure homogeneity of the modifier elements throughout thealumina material.

The modified alumina materials of this invention are characterized as:(i) having a concentration of modifier component ranging from about 10to about 5000 wppm; (ii) a surface area greater than about 50 m² /g,preferably from about 100 to 700 m² /g, and more preferably from about100 to 300 m² /g; (iii) a bulk density from about 0.3 to 1 g/ml,preferably from about 0.4 to 0.8 g/ml; (iv) an average pore volume fromabout 0.2 to 1.1 ml/g, preferably from about 0.3 to 0.8 ml/g; and (v) anaverage pore diameter from about 30 to 300 Angstroms.

A unique feature of the modified aluminas of the present invention aretheir attenuated acidic character relative to conventional, reforminggrade aluminas, such as high purity gamma alumina. While these differingacidities may be assessed by various analytical procedures, one of themost definitive procedures is the chemistry of the catalytic reformingprocess as it is in this environment where the influence of the aluminaacid function is observed. In this sense, heptane reforming serves as amodel system for observing and quantifying the role of the supportacidity on reforming selectivity and activity. While various metal siteand acid site cracking reactions occur giving rise to different sets ofreaction products from heptane, only cracking to isobutane isexclusively diagnostic of acid cracking activity. For this reason,changes in the isobutane yield in heptane reforming reflect changes inthe acid character of the catalyst, and this product yield in itself candistinguish among catalysts with differing acid strengths and productselectivities. Furthermore, this measure is further refined bycomparison of the toluene/isobutane ratios for various catalysts, forthis value invariably increases as toluene and C₅ + selectivity increaseas isobutane yield decreases. While the toluene/isobutane ratio is mostvalid for comparison of the same metal, or metals, supported on aluminasof varying acidity, the generalization can be made that for heptanereforming, the catalysts supported on the modified alumina of thisinvention result in at least about 10 wt. % less isobutane yield,preferably at least about 20 wt. % less isobutane yield; and at leastabout 5% greater toluene to isobutane ratio, preferably at least about10% toluene to isobutane ratio, when compared with the identicalcatalyst on conventional high purity gamma alumina.

A reforming catalyst is prepared from the modified aluminas of thepresent invention by incorporating therein at least one metal capable ofproviding a hydrogenation-dehydrogenation function. The resultingcatalysts will also contain a cracking function which is important forisomerization reactions and which is associated with the modifiedalumina support material. The hydrogenation-dehydrogenation function ispreferably provided by at least one Group VIII noble metal, preferablyplatinum. Preferably, the platinum group metal will be present on thecatalyst in an amount from about 0.01 to about 2 wt. %, calculated on anelemental basis, of the final catalyst composition. More preferably, thecatalyst contains from about 0.1 to about 0.7 wt. % platinum, mostpreferably about 0.3 to 0.6 wt. % platinum. The catalysts of the presentinvention will also contain from 0.01 to 2 wt. % Ir, preferably 0.1 to0.7 wt. % Ir, and more preferably from 0.3 to 0.6 wt. % Ir. The iridiumcomponent of the catalysts of the present invention is agglomerated tosuch an extent to exhibit a crystallinity greater than about 50 percent,preferably greater than about 75 percent, and more preferably about 100percent, as measured by x-ray diffraction. That is, greater than about50 percent, preferably greater than about 75 percent, and morepreferably substantially all of the iridium component, based on thetotal weight of the iridium component, is present on the catalyst asiridium crystallites having a crystallite size greater than about 30Angstrom Units, as measured by x-ray diffraction.

The catalysts of the present invention may also contain up to about 2wt. % of one or more additional metal, other than the alumina modifiercomponent. The other metal is one selected from copper, tin, rhenium,palladium, rhodium, tungsten, ruthenium, osmium, silver, gold, gallium,lead, bismuth, antimony and the like. Preferred are rheniuma and tin,preferably in an amount ranging from about 0.1 to about 0.7 wt. %, morepreferably from about 0.3 to about 0.6 wt. %.

Conventional iridium promoted platinum catalysts used in reforminggenerally show substantially no crystallinity since the iridium is welldispersed on the support and the crystallites sizes are well below thephysical detectable limit of about 30 Angstrom Units. Evidence ofcrystallites of well dispersed iridium catalysts is substantiated bychemical techniques, but because of their small sizes, they aregenerally not detectable by x-ray diffraction or electron microscopy.Beyond about 30 Angstrom Units, the crystallites become detectable byx-ray diffraction. It was historically believed that agglomeration ofiridium on a reforming catalyst should be avoided; thus it was onlyrecently that this researcher discovered that as the iridiumagglomerates and the crystallite sizes become greater and the iridiumcomponent exhibits a crystallinity greater than about 50 percent, theproperties of the iridium promoted platinum catalysts begin to improve,often to the extent that they are equal to, or greater than, anotherwise equivalent platinum-iridium catalyst except for its iridiumcomponent being well dispersed. A detailed discussion of agglomeratediridium-platinum reforming catalysts can be found in U.S. Pat. No.4,701,255; which is incorporated herein by reference.

The iridium component can be agglomerated in virtually any appropriatemethod. One method is to heat the iridium-containing alumina support,prior to, or after, the addition of the platinum component, attemperatures in excess of about 425° C., in the presence of air oroxygen. Such excessive temperatures, in the presence of oxygen, aregenerally avoided in the art to prevent, or suppress, iridiumagglomeration. Thus, for purposes of this invention, iridium can beimpregnated, or otherwise dispersed, onto the modified alumina, thencalcined in air at temperatures in excess of about 425° C., preferably455° C., and more preferably 485° C., for about three or more hours. Apreferred technique for forming the catalysts of this invention is todisperse the iridium into the modified alumina material, agglomeratesame, and then add the platinum and optionally another metal componentby conventional techniques, suitably by impregnation. The platinumagglomeratediridium modified alumina catalyst can then be recalcined inair at generally similar conditions for from about 1 to about 24 hours,then reduced, suitably with a flowing stream of hydrogen at from about485° C. to about 510° C., and then sulfided, suitably by contact with ahydrogen sulfide containing gas, e.g., an H₂ S/H₂ blend, to sulfurbreakthrough from the exit side of the catalyst bed. Conversely, theorder of addition of the platinum and iridium can be reversed. Thus, theplatinum and iridium, in that order, can be sequentially impregnatedonto the support and then treated as described to agglomerate theiridium component. Alternatively, the platinum and iridium can becoimpregnated and the catalyst then calcined in air, or anoxygen-containing gas at about 425° C. to about 510° C., preferablyabout 480° C. to about 510° C., and then reduced and sulfided asdescribed.

Suitably, the platinum-iridium and other metal components, if any, canbe deposited by impregnation on the modified alumina which waspreviously pilled, pelleted, beaded, or extruded. It can also beincorporated into the so-called mull mix, or paste, prior to extrusion.If impregnation is used, the modified alumina, in a dry, or solvatedstate, is contacted, either alone or admixed, or otherwise incorporatedwith platinum-iridium and other metal component, if any, or a platinumcontaining solution and thereby impregnated by either the "incipientwetness" technique, or a technique embodying absorption from a dilute orconcentrated solution, with subsequent filtration or evaporation toeffect the total uptake of the metallic components. The solution used inthe impregnation step can be a salt or acid solution having therespective platinum and iridium compound dissolved therein. The amountof impreganation solution used should be sufficient to completelyimmerse the alumina. This is usually within the range of about 1 to 20times the amount of alumina, by volume, depending on the platinumconcentration in the impregnation solution. The impregnation treatmentcan be carried out under a wide range of conditions, including ambientor elevated temperatures, and atmospheric or superatmospheric pressures.

The catalyst may also contain a halide component which contributes tothe acid functionality of the catalyst. The halide may be fluoride,chloride, iodide, bromide, or mixtures thereof. Preferred are fluorideand chloride, with chloride being more preferred. Generally, the amountof halide is such that the final catalyst composition will contain fromabout 0.1 to about 3.5 wt. %, preferably from about 0.5 to about 1.5 wt.%, of halogen calculated on an elemental basis. The halogen can beintroduced into the catalyst by any method at any time of the catalystpreparation, for example, prior to, following or simultaneously with theimpregnation of the metals. In the usual operation, the halogencomponent is introduced simultaneously with the incorporation ofplatinum. Halogen can also be incorporated by contacting the modifiedalumina in a vapor phase, or liquid phase, with a halogen compound suchas hydrogen fluoride, hydrogen chloride, ammonium chloride, or the like.

The catalyst, after impregnation, is dried by heating at a temperatureabove about 27° C., preferably between about 65° C. and 150° C., in thepresence of nitrogen or oxygen, or both, in an air stream or undervacuum. It can then be calcined at a temperature from about 400° C. to650° C., preferably from about 400° C. and 560° C., in the presence ofnitrogen or oxygen in an air stream, or in the presence of a mixture ofoxygen and an inert gas. This calcination or activation is conducted forperiods ranging from about 1 to about 24 hours in either flowing orstatic gases. Reduction is performed by contact with flowing hydrogen attemperatures ranging from about 175° C. to about 560° C. for periodsranging from about 0.5 to about 24 hours at about 1-40 atm. The catalystcan be sulfided by use of a blend of H₂ S/H₂ and performed attemperature ranging from about 175° C. to about 560° C. at about 1-40atm. for a time necessary to achieve breakthrough, or until the desiredsulfur level is reached. Post-sulfiding stripping can be employed, ifdesired, at conditions similar to those for reduction of the catalyst.

The feed, or charge stock can be a virgin naphtha, cracked naphtha, aFischer-Tropsch naphtha, or the like. Typical feeds are thosehydrocarbons containing from about 5 to 12 carbon atoms, or morepreferably from about 6 to about 9 carbon atoms. Naphthas, or petroleumfractions boiling within the range of from about 27° C. to 235° C., andpreferably from about 50° C. and 190° C., contain hydrocarbons of carbonnumbers within these ranges. Typical fractions thus usually contain fromabout 20 to about 80 vol. % paraffins, both normal and branched, whichfall in the range of about C₅ to C₁₂ ; from about 10 to 80 vol. % ofnaphthenes falling within the range of from about C₆ to C₁₂ ; and from 5through 20 vol. % of the desirable aromatics falling within the range offrom about C₆ to C₁₂.

The reforming runs are initiated by adjusting the hydrogen and feedrates, and the temperature and pressure to operating conditions. The runis continued at optimum reforming conditions by adjustment of the majorprocess variables, within the ranges described below:

    ______________________________________                                        Major Operating                                                                              Typical Process                                                                           Preferred Process                                  Variables      Conditions  Conditions                                         ______________________________________                                        Pressure, Psig  50-750     100-300                                            Reactor Temp., °C.                                                                    400-600     465-540                                            Gas Rate, SCF/B                                                                                1500-10,000                                                                             2000-7000                                          (Incl. Recycle Gas)                                                           Feed Rate, W/Hr/W                                                                            0.5-10      1-3                                                ______________________________________                                    

The instant invention is illustrated further by the following exampleswhich, however, are not to be taken as limiting in any respect. Allparts and percentages, unless expressly stated otherwise, are by weight.

COMPARATIVE EXAMPLE A

A commercial Pt reforming catalyst (0.3 wt. % Pt, 0.9 wt. % Cl) on ahigh purity gamma alumina was calcined in air at 500° C. for 3 hrs.,reduced at 500° C. for 17 hrs. in hydrogen, and sulfided at 500° C. ThisPt catalyst, Catalyst A, was tested in heptane reforming with theresults presented in Table I below.

EXAMPLE 1

An alumina of this invention was used containing 200 wppm Na, 150 wppmCa, 146 wppm Mg, 480 wppm Fe, and 500 wppm Si. Extrudates of thismaterial (50 g.) were mixed with 75 ml. of water and placed in a frittedfunnel whereupon carbon dioxide was passed through it for 30 minutes. Tothe mixture was added 5.4 ml. of chloroplatinic acid (28 mg Pt/ml.) and4.8 ml. of hydrochloric acid (60 mg Cl/ml.) and carbon dioxide passedthrough it for 4 hours. The resulting catalyst was air dried, thenvacuum dried at 110° C. for 4 hours. The catalyst was then calcined inair at a temperature of 500° C. for 3 hours, then reduced in hydrogen at500° C. for 17 hours, then sulfided in a mixture of hydrogen sulfide andhydrogen at 500° C. until sulfur breakthrough. This catalyst isdesignated Catalyst B, and contains 0.3 wt. % Pt and 0.9 wt. % Cl., andwas tested in heptane reforming with the results presented in Table Ibelow.

EXAMPLE 2

A preferred catalyst of this invention was prepared by the addition ofPt to an alumina modified by the addition of Mg and Si during itsmanufacture. In this case 500 ppm Mg and 500 ppm Si were added to thealumina mull mix preceding extrusion. The ingredients were thoroughlyblended and mixed in the mull mixer, then passed to the extruder. Theresultant extrudates were calcined at 600°-700° C. Pt was impregnatedonto the Mg/Si modified alumina as in Example 1 above to provide a 0.3wt. % Pt on modified alumina catalyst. The catalyst was also pretreatedas in Example 1 and subjected to heptane reforming and is designated asCatalyst C in Table I below.

COMPARATIVE EXAMPLE B

A commercial reforming catalyst containing 0.6 wt. % Pt and 0.9 wt. %Cl, on a high purity alumina support was calcined, reduced, and sulfidedas in Example 1 above. This catalyst is designated Catalyst D, and wasalso tested in heptane reforming and the results presented in Table Ibelow.

EXAMPLE 3

The procedure of Example 1 was followed except the catalyst contained0.6 wt. % Pt and 0.9 wt. % Cl. The catalyst of this example, which iscomprised of the alumina of Example 1 hereof, is designated Catalyst E.Heptane reforming data was collected and the results are also shown inTable I below.

                  TABLE I                                                         ______________________________________                                        Heptane Reforming With Pt Catalysts                                           n-Heptane, 500° C., 100 psig, 10 W/H/W, H.sub.2 /Oil = 6               Catalyst    A        B      C      D    E                                     ______________________________________                                        Yield, Wt. %                                                                  C.sub.1     1.2      0.9    1.1    1.6  1.0                                   i-C.sub.4   6.0      2.5    2.5    2.5  1.9                                   n-C.sub.4   5.1      3.4    3.7    4.7  3.3                                   C.sub.5 +   76.4     86.6   86.1   82.5 87.9                                  Toluene     28.6     24.6   27.7   28.2 28.1                                  Conversion, %                                                                             64.5     48.1   55.5   62.4 49.5                                  Toluene Rate                                                                              2.9      2.5    2.9    3.3  2.9                                   Toluene     43.9     50.4   49.6   50.7 56.3                                  Selectivity                                                                   Toluene/i-C.sub.4                                                                         4.8      9.8    11.1   11.3 14.8                                  ______________________________________                                    

Table I illustrates that Catalysts B and C, supported on modifiedaluminas of this invention, have a totally different selectivity patternfrom conventional Catalyst A, which is on a high purity conventionalgamma alumina. Acid cracking for the catalysts of this invention isgreatly decreased as reflected in the isobutane yields. A secondaryeffect is a decrease in Pt hydrocracking reactions. The combineddecrease in all cracking reactions leads to a 10 wt. % increase in theC₅ + yield with improved selectivity to toluene. The toluene/isobutaneratios for Catalyst A and B differ substantially, with it being higherfor the catalyst (B), of this invention. The difference lies in thiscase in greatly reduced isobutane yield for Catalyst B.

While Catalysts B and C are catalysts of this invention, atalyst Crepresents a catalyst which is preferred over Catalyst B. Catalyst C, acatalyst containing substantially no Na or Fe, is more active thanCatalyst B, while exhibiting a substantial C₅ ⁺ selectively credit ofabout 10.0 wt. %. Catalyst C also has the higher toluene/isobutane ratiocharacteristics of preferred catalysts of this invention, which accountsfor its improved selectivity.

Comparison of Catalysts D and E shows the same selectivity advantages,but at the higher Pt loading, indicating that the influence of themodified alumina of this invention is independent of Pt loading. Thetoluene/isobutane ratios of these two catalysts show the expected shiftto a higher level for Catalyst E, which also has higher C₅ + and tolueneselectivities.

COMPARATIVE EXAMPLE C

A commercial reforming catalyst comprised of 0.3 wt. % Pt, 0.3 wt. % Re,and 0.9wt. % Cl on high purity gamma alumina was calcined in air at 500°C. for 3 hrs., reduced for 17 hrs. in hydrogen, then sulfided, all at atemperature of 500° C. This catalyst, designated Catalyst F, was testedfor heptane reforming with the results presented in Table II below.

COMPARATIVE EXAMPLE D TO I

Various amounts of Na, Fe, Ca, and Mg were impregnated into the highpurity gamma alumina prior to impregnation of 0.3 wt. % Pt, 0.3wt. % Re,and 0.9 wt. % Cl. After impregnation of the modfier the alumina wascalcined in air at 500° C. for 3 hrs. The metals and Cl were thenimpregnated into the modified alumina, after which it was calcined,reduced and sulfided as in Example 1 above. All of the catalysts (G-L)were tested in heptane reforming and the results are shown in Table IIbelow.

EXAMPLE 4

Catalyst M was prepared in accordance with Example 1 hereof except that3.8 ml of Re stock solution (42 mg Re/ml) was used to incorporate 0.3wt. % Re into the modified alumina support. This catalyst, whichcontained 0.3 wt. % Pt and 0.3 wt. % Re, was also tested for heptanereforming and the results shown in Table II below.

COMPARATIVE EXAMPLE J

A sample of high purity reforming grade gamma alumina was impregnatedwith magnesium nitrate to give 420 ppm of Mg on alumina. The extrudateswere calcined at 950° F. for 3 hrs., then impregnated with 5.4 ml. ofchloroplatinic acid (28 mg Pt/ml) and 3.8 ml. of Re stock solution (42mg Re/ml), and 4.8 ml of hydrochloric acid to give a catalyst comprisedof 0.3 wt. % Pt, 0.3 wt. % Re, 0.9 wt. % Cl, and 420 ppm Mg on alumina.This catalyst, Catalyst N, was also tested for heptane reforming and theresults given in Table II below.

COMPARATIVE EXAMPLE K

Catalyst O was prepared in accordance with the procedure of ComparativeExample J hereof except that 500 ppm Si was impregnated into thecatalyst. This catalyst was also tested for heptane reforming and theresults are shown in Table II below.

EXAMPLE 5

Catalyst P was prepared by modifying a high purity gamma alumina mullmix with 500 ppm Mg and 500 ppm Si. The modified alumina was thenextruded, the resulting extrudes calcined at a temperature between about600°-700° C. after which 0.3 wt. % Pt, 0.3 wt. % Re, and 0.9 wt. % Clwere impregnated into the extrudates as in Comparative Example J above.This catalyst, which was pretreated by calcining in air for 3 hrs.,reducing in hydrogen for 17 hrs., and sulfided, all at 500° C., was alsotested for heptane reforming and the results shown in Table II below.

                                      TABLE II                                    __________________________________________________________________________    Heptane Reforming                                                             n-Heptane, 500° C., 100 psig, 10 W/H/W, H.sub.2 /Oil = 6               Example C  D  E  F  G  H  I  4  J  K  5                                       Catalyst                                                                              F  G  H  I  J  K  L  M  N  O  P                                       __________________________________________________________________________    Na, wppm                                                                              <20                                                                              110                                                                              <20                                                                              <20                                                                              <20                                                                              <20                                                                              <20                                                                              200                                                                              <20                                                                              <20                                                                              <20                                     Fe, wppm                                                                              <20                                                                              <50                                                                              670                                                                              <50                                                                              830                                                                              <50                                                                              870                                                                              480                                                                              <50                                                                              <50                                                                              <50                                     Ca, wppm                                                                              <20                                                                              <20                                                                              <20                                                                              234                                                                              724                                                                              <20                                                                              <20                                                                              150                                                                              <20                                                                              <20                                                                              <20                                     Mg, wppm                                                                              <20                                                                              <20                                                                              <20                                                                              <20                                                                              <20                                                                              330                                                                              360                                                                              146                                                                              420                                                                              <20                                                                              500                                     Si, wppm                                                                              <20                                                                              <20                                                                              <20                                                                              <20                                                                              <20                                                                              <20                                                                              <20                                                                              500                                                                              <20                                                                              500                                                                              500                                     Yield, Wt. %                                                                  C.sub.1 1.4                                                                              1.3                                                                              1.2                                                                              1.4                                                                              1.1                                                                              1.3                                                                              1.1                                                                              1.3                                                                              1.4                                                                              1.3                                                                               1.4                                    i-C.sub.4                                                                             3.3                                                                              2.6                                                                              2.9                                                                              2.5                                                                              2.7                                                                              2.3                                                                              2.2                                                                              2.3                                                                              2.6                                                                              3.4                                                                              2.8                                     n-C.sub.4                                                                             5.5                                                                              5.6                                                                              5.0                                                                              5.6                                                                              5.0                                                                              5.4                                                                              4.6                                                                              5.2                                                                              5.6                                                                              5.3                                                                              5.3                                     C.sub.5 +                                                                             79.7                                                                             81.4                                                                             82.0                                                                             81.1                                                                             82.4                                                                             82.1                                                                             84.2                                                                             82.7                                                                             81.2                                                                             79.9                                                                             81.2                                    Toluene 31.3                                                                             24.3                                                                             25.0                                                                             27.7                                                                             24.8                                                                             26.9                                                                             22.2                                                                             25.9                                                                             27.7                                                                             30.0                                                                             28.4                                    Conversion, %                                                                         65.3                                                                             55.3                                                                             55.1                                                                             59.4                                                                             54.0                                                                             57.0                                                                             48.7                                                                             55.1                                                                             59.3                                                                             63.7                                                                             60.0                                    Toluene Rate                                                                          3.2                                                                              2.5                                                                              2.6                                                                              2.8                                                                              2.5                                                                              2.8                                                                              2.3                                                                              2.7                                                                              2.8                                                                              3.1                                                                              2.9                                     Toluene 48.0                                                                             44.1                                                                             45.4                                                                             46.6                                                                             45.9                                                                             47.2                                                                             48.7                                                                             47.0                                                                             46.7                                                                             47.1                                                                             47.4                                    Selectivity                                                                   Toluene/i-C.sub.4                                                                     9.5                                                                              9.4                                                                              8.6                                                                              11.1                                                                             9.2                                                                              11.7                                                                             10.0                                                                             11.3                                                                             10.7                                                                             8.8                                                                              10.1                                    __________________________________________________________________________

The data of the above table are best understood by reference to FIGS. 1and 2 hereof exhibiting catalyst activity and stability as a function oftime. Catalyst O, which contains only Si as the modifier, shows thehighest activity as shown in FIG. 1. While Catalyst F, the referencecommercial catalyst has comparable initial activity, it is relativelyunstable, and its activity decreases with time. Catalyst N, whichcontains only Mg as the modifier, has a similar activity profile butbeing about 5 to 10% less active than Catalyst F. FIG. 2 hereof showsCatalyst N as having the highest yield and yield stability, whileCatalyst O, as a consequence of its improved stability, shows a yieldbenefit over Catalyst F, but trails that of Catalyst N. If FIGS. 1 and 2are considered together, one sees that only Catalyst P, which containsboth Si and a Group II-A metal, affords activity, yield, and stabilitycharacteristics that are absent in the other catalysts.

The above table also illustrates the effectiveness of the modifiers ofthis invention versus such use of such metals as Na and Fe which are atbest are relatively ineffective, though still representing catalysts ofthis invention.

COMPARATIVE EXAMPLE L

A conventional reforming catalyst comprised of 0.3 wt. % Pt; 0.7 wt. %Re, 0.9 wt. % Cl, on high purity alumina was pretread as in ComparativeExample A above. The catalyst, designated Catalyst Q, was also used forheptane reforming and the results shown in Table III below.

EXAMPLE 6

Catalyst R was prepared by impregnating 0.3 wt. % Pt and 0.7 wt. % Reinto the Mg/Si modified alumina support of Example 2 hereof. Thiscatalyst was also tested for heptane reforming and the results presentedin Table III below.

                  TABLE III                                                       ______________________________________                                        Heptane Reforming With                                                        0.3 Wt. % Pt-0.7 Wt. % Re Catalysts                                           n-Heptane, 500° C., 100 psig, 10 W/H/W, H.sub.2 /Oil = 6               Catalyst           O      R                                                   ______________________________________                                        Yield, Wt. %                                                                  C.sub.1            1.4    1.1                                                 i-C.sub.4          6.4    3.8                                                 n-C.sub.4          5.7    6.0                                                 C.sub.5 +          73.0   78.5                                                Toluene            28.2   19.2                                                Conversion, %      71.9   57.0                                                Toluene Rate       2.9    2.0                                                 Toluene Selectivity                                                                              39.2   33.8                                                Toluene/i-C.sub.4  4.4    5.1                                                 ______________________________________                                    

Catalyst R of this invention has selectivity advantages over thecommercial Catalyst Q. The C₅ ⁺ selectivity credit arises from decreasedacid cracking over Catalysts R. The toluene/i-C₄ ratios reflect thisdistinction and are higher for Catalyst R supported on the modifiedalumina.

COMPARATIVE EXAMPLES M

Catalyst S was prepared by pretreating a conventional reforming catalystcomprised of 0.3 wt. % Pt and 0.3 wt. % Ir on high purity gamma alumina,by calcining it in air at a temperature of 400° F. for 3 hrs., followedby reducing it in hydrogen at 500° C. for 17 hrs., followed by sulfidingat 500° C. This catalyst was tested in heptane reforming and the resultsare found in Table IV below.

COMPARATIVE EXAMPLE N

High purity gamma alumina extrudates were impregnated with an aqueousmagnesium nitrate solution to provide 210 wppm Mg. The extrudates werethen calcined at about 500° C. for 3 hrs. then impregnated, as inExample 1 hereof, with a solution containing Pt and Ir to give 0.3 wt. %Pt and 0.3 wt. % Ir, based on the final weight of the catalyst. The sotreated extrudates were then pretreated as in Comparative Example Mabove and the resulting catalyst (T) was tested in heptane reforming,the results of which are also found in Table IV below.

EXAMPLE 7

500 wppm Mg and 500 wppm Si were added to a high purity gamma aluminamull mix preceding extrusion. The mix was thoroughly blended in the mullmixer then extruded. The resulting extrudates were then calcined in airat a temperature between 600° C. and 700° C., after which 0.3 wt. % Ptand 0.3 wt. % Ir were impregnated as in Example 1 hereof. The soimpregnated extrudates were then pretreated as in Comparative Example Mabove and the resulting catalyst (U) was also tested in heptanereforming. The results are shown in Table IV below.

                  TABLE IV                                                        ______________________________________                                        Heptane Reforming With Modified Pt-Ir Catalysts                               n-Heptane, 500° C., 100 psig, 10 W/H/W, H.sub.2 /Oil = 6               Catalyst       S          T      U                                            ______________________________________                                        Na, wppm       <20        <20    <20                                          Ca, wppm       <20        <20    <20                                          Mg, wppm       <20        210    500                                          Fe, wppm       <20        <20    <20                                          Si, wppm       <20        <20    500                                          Yield, Wt. %                                                                  C.sub.1        1.8        1.9    1.7                                          i-C.sub.4      2.8        1.5    1.8                                          n-C.sub.4      5.0        5.3    4.7                                          C.sub.5 +      80.4       82.4   83.5                                         Toluene        29.0       25.7   24.9                                         Conversion, %  62.3       56.7   54.3                                         Toluene Rate   6.0        5.3    5.1                                          Toluene Selectivity                                                                          62.3       56.7   45.9                                         Toluene/i-C.sub.4                                                                            10.4       17.1   13.9                                         ______________________________________                                    

COMPARATIVE EXAMPLE O

Comparative Example M was repeated except the catalyst contained 0.6 wt.% Pt and 0.6 wt. % Ir on high purity alumina. The resulting catalyst (V)was tested in heptane reforming and the results are shown in Table Vbelow.

COMPARATIVE EXAMPLE P

Comparative Example N was followed except the catalyst contained 0.6 wt.% Pt, 0.6 wt. % Ir, and 350 wppm Mg on high purity gamma alumina. Theresulting catalyst (W) was also tested in heptane reforming with theresults are shown in Table V below.

EXAMPLE 8

Example 7 hereof was followed except the catalyst was comprised of 0.6wt. % Pt, 0.6 wt. % Ir, 500 wppm Mg, and 500 wppm Si on alumina. Thiscatalyst (X) was also tested in heptane reforming and the results areshown in Table V below.

                  TABLE V                                                         ______________________________________                                        Heptane Reforming With Modified Pt-Ir Catalysts                               n-Heptane, 500° C., 100 psig, 10 W/H/W, H.sub.2 /Oil = 6               Catalyst       V          W      X                                            ______________________________________                                        Na, wppm       <20        <20    <20                                          Ca, wppm       <20        <20    <20                                          Mg, wppm       <20        350    500                                          Fe, wppm       <20        <20    <20                                          Si, wppm       <50        <50    500                                          Yield, Wt. %                                                                  C.sub.1        2.4        2.4    2.0                                          i-C.sub.4      2.9        2.0    2.1                                          n-C.sub.4      6.4        6.1    5.6                                          C.sub.5 +      75.9       78.7   80.7                                         Toluene        30.8       31.2   30.2                                         Conversion, %  70.0       67.8   63.8                                         Toluene Rate   6.3        6.4    6.2                                          Toluene Selectivity                                                                          44.3       45.7   47.4                                         Toluene/i-C.sub.4                                                                            10.6       15.6   14.4                                         ______________________________________                                    

COMPARATIVE EXAMPLE O

The procedure of Example 1 hereof was followed to prepare a trimetalliccatalyst (Y) comprised of 0.3 wt. % Pt, 0.3 wt. % Ir, and 0.3 wt. % Reon high purity gamma alumina. The catayst was pretreated as inComparative Example N hereof and tested in heptane reforming. Theresults are shown in Table VI below.

EXAMPLE 9

The procedure of Example 1 was followed except the alumina contained 200wppm Na, 150 wppm Ca, 146 wppm Mg, 480 wppm Fe, and 500 wppm Si, as wellas 0.3 wt. % Pt, 0.3 wt. % Ir, and 0.3 wt. % Re. The catalyst (Z) wasalso tested in heptane reforming and the results are shown in Table VIbelow.

                  TABLE VI                                                        ______________________________________                                        Heptane Reforming With Modified Pt-Ir Catalysts                               n-Heptane, 500° C., 100 psig, 10 W/H/W, H.sub.2 /Oil = 6               Catalyst           Y      Z                                                   ______________________________________                                        Na, wppm           <20    200                                                 Ca, wppm           <20    150                                                 Mg, wppm           <20    146                                                 Fe, wppm           <20    480                                                 Si, wppm           <50    500                                                 Yield, Wt. %                                                                  C.sub.1            1.6    1.2                                                 i-C.sub.4          2.9    1.5                                                 n-C.sub.4          5.3    3.8                                                 C.sub.5 +          80.1   86.9                                                Toluene            31.6   22.9                                                Conversion, %      64.6   46.4                                                Toluene Rate       6.5    4.7                                                 Toluene Selectivity                                                                              48.9   49.4                                                Toluene/i-C.sub.4  10.9   15.3                                                ______________________________________                                    

COMPARATIVE EXAMPLE R

An agglomerated Pt-Ir catalyst (AA) was prepared by following theprocedure of Example 1 hereof using high purity gamma alumina. Theimpregnation mixture contained 8.9 ml. of Pt stock solution and 3.1 mlof Ir stock solution, to give a 0.5 wt. % Pt - 0.1 wt. % Ir content.After being air and vacuum dried, the catalyst was calcined in air at500° C. for 3 hrs. to agglomerate the Ir. The catalyst was then reducedat about 500° C. for 17 hours then sulfided at the same temperature. Theresulting catalyst was then tested in heptane reforming, the results ofwhich are found in Table VII below.

EXAMPLE 10

The procedure of Comparative Example R was followed except the aluminawas a modified alumina as in Example 1 hereof. The resulting catalyst(AB) was tested for heptane reforming and the results are found in TableVII below.

                  TABLE VII                                                       ______________________________________                                        Heptane Reforming With Agglomerated Pt-Ir Catalysts                           n-Heptane, 500° C., 100 psig, 20 W/H/W, H.sub.2 /Oil = 6               Catalyst           AA     AB                                                  ______________________________________                                        Na, wppm           <20    200                                                 Ca, wppm           <20    150                                                 Mg, wppm           <20    146                                                 Fe, wppm           <20    480                                                 Si, wppm           <20    500                                                 Yield, Wt. %                                                                  C.sub.1            1.6    0.9                                                 i-C.sub.4          2.8    1.4                                                 n-C.sub.4          4.6    3.6                                                 C.sub.5 +          82.0   88.8                                                Toluene            30.5   21.4                                                Conversion, %      61.7   41.1                                                Toluene Rate       6.2    4.4                                                 Toluene Selectivity                                                                              49.0   51.8                                                Toluene/i-C.sub.4  10.9   15.3                                                ______________________________________                                    

Table VII illustrates that agglomerated Pt-Ir catalysts exhibit the sameresponse to the alumina supports of this invention as the Pt-Re andPt-Ir series. That is, the C₅ + selectivity is improved, and thetoluene/isobutane ratio increases for the catalyst of this invention,Catalyst AB.

COMPARATIVE EXAMPLE S

A 0.5 wt. % Pt - 0.3 wt. % Re - 0.1 wt. % Ir Catalyst (AC), was preparedin accordance with the procedure of Example 1 hereof except that highpurity gamma alumina was used. After being dried, the catalyst wascalcined in air at 500° C. for 3 hrs. to agglomerate the Ir. It was thenreduced in a hydrogen containing atmosphere at a temperature of about500° C. for 17 hours, then sulfided at the same temperature. The resultsof the heptane reforming are found in Table VIII below.

EXAMPLE 11

Catalyst AD was prepared in accordance with procedure of ComparativeExample S except the alumina was the modified alumina of Example 1hereof. The results of heptane reforming are found in Table VIII below.

                  TABLE VIII                                                      ______________________________________                                        Heptane Reforming With Agglomerated Ir-Pt-Re Catalysts                        n-Heptane, 500° C., 100 psig, 10 W/H/W, H.sub.2 /Oil = 6               Catalyst           AC     AD                                                  ______________________________________                                        Na, wppm           <20    200                                                 Ca, wppm           <20    150                                                 Mg, wppm           <20    146                                                 Fe, wppm           <20    480                                                 Si, wppm           <50    500                                                 Yield, Wt. %                                                                  C.sub.1            1.3    1.1                                                 i-C.sub.4          2.0    1.2                                                 n-C.sub.4          4.8    4.4                                                 C.sub.5 +          83.4   86.6                                                Toluene            27.8   23.1                                                Conversion, %      55.7   46.2                                                Toluene Rate       5.7    4.7                                                 Toluene Selectivity                                                                              49.9   49.9                                                Toluene/i-C.sub.4  13.9   19.3                                                ______________________________________                                    

Table VIII illustrates that the agglomerated trimetallic supported onthe alumina of this invention has a higher C₅ + selectively andtoluene/isobutane ratio than its counterpart supported on conventionalalumina.

COMPARATIVE EXAMPLE T

Catalyst AE was prepared by incorporating 0.3 wt. % Sn in a mull mix ofhigh purity alumina. The mull mix was then extruded, the extrudatesdried, then impregnated with 0.6 wt. % Pt and 0.6 wt. % Ir by using amixture containing 10.8 ml of Pt stock solution and 17.6 ml of Ir stocksolution, and 5 ml of chloride stock solution. The resulting catalystwas calcined at about 400° C. for 3 hrs., reduced at about 500° C. for17 hrs., then sulfided at about 500° C. This catalyst was also tested inheptane reforming and the results are found in Table IX below.

EXAMPLE 12

The above procedure was followed except instead of high purity alumina,the alumina contained about 200 wppm Na, 150 wppm Ca, 146 wppm Mg, 480wppm Fe, and 500 wppm Si. The catalyst (AF) was also tested in heptanereforming and the results are found in Table IX below.

COMPARATIVE EXAMPLE U

The procedure of Comparative Example T was followed except the resultingcatalyst was comprised of 0.3 wt. % Pt - 0.1 wt. % Ir - 0.1 wt. % Sn onhigh purity gamma alumina. The catalyst (AG) was calcined at 500° C. for3 hrs. to agglomerate the Ir prior to reduction and sulfiding. Theheptane reforming date is also found in Table IX below.

EXAMPLE 13

Catalyst AH was prepared by the procedure of Comparative Example Texcept the alumina was the modified alumina of Example 1 hereof and thecatalyst contained 0.3 wt. % Pt - 0.1 wt. % Ir - 0.1 wt. % Sn. Theheptane reforming data is found in Table IX below.

                  TABLE IX                                                        ______________________________________                                        Heptane Reforming With Pt-Ir-Sn Catalysts                                     n-Heptane, 500° C., 100 psig, 20 W/H/W, H.sub.2 /Oil = 6               Catalyst       AE     AF        AG   AH                                       ______________________________________                                        Na, wppm       <20    200       <20  200                                      Ca, wppm       <20    150       <20  150                                      Mg, wppm       <20    146       <20  146                                      Fe, wppm       <20    480       <20  480                                      Si, wppm       <50    500       <50  500                                      Yield, Wt. %                                                                  C.sub.1        1.6    1.2       0.8  0.7                                      i-C.sub.4      3.2    1.5       2.5  1.9                                      n-C.sub.4      5.3    4.1       3.5  3.1                                      C.sub.5 +      79.4   86.2      85.7 87.5                                     Toluene        31.3   21.7      22.1 20.3                                     Conversion, %  66.1   45.8      46.1 41.4                                     Toluene Rate   6.4    4.5       4.5  4.2                                      Toluene Selectivity                                                                          47.4   47.6      47.9 49.0                                     Toluene/i-C.sub.4                                                                            9.8    14.5      8.8  10.7                                     ______________________________________                                    

Various samples of the above catalysts were used to reform a Light Arabparaffinic naphtha at high severity cyclic conditions of 500° C., 140psig, 2200 SCF/B, 1.9 W/H/W. The results are shown in Table X below.

                  TABLE X                                                         ______________________________________                                        Cyclic Reforming of                                                           Low Sulfur Light Arab Paraffinic Naphtha                                                        C.sub.5 + LV %                                                                           Decrease in                                      Catalyst Activity at 100 RON C.sub.3 /C.sub.4 Wt. % (a)                       ______________________________________                                        F         74      71.8       --                                               N         77      75.0       3.1                                              P         90      74.0       2.2                                              AG       117      75.8       --                                               AH       100      76.5       1.8                                              Y        118      76.5       --                                               Z        121      78.5       1.4                                              ______________________________________                                         (a) Decrease relative to same catalyst on conventional reforming alumina.

The above table illustrates that the catalysts of the present invention,P, AH and Z have a substantially increased activity or increased liquidyield over the reference catalysts.

What is claimed is:
 1. In a method for reforming naphtha feeds, in the presence of hydrogen and at reforming conditions, the improvement which comprises using a catalyst composition comprised of: about 0.01 to 2 wt. % platinum; about 0.01 to 2 wt. % iridium agglomerated to exhibit a crystallinity greater than 50 percent, as measured by x-ray; up to about 2 wt. % of rhenium; up to about 2 wt. % of tin; up to 3.5 wt. % of a halide, and the balance being alumina modified with at least about 100 wppm of Si and at least about 10 wppm of one or more alkaline-earth metals selected from Ca, Mg, Ba, and Sr, wherein the total amount of modifier does not exceed about 5000 wppm.
 2. The method of claim 1 wherein about 0.1 to 0.7 wt. % of each of platinum and iridium are present and the crystallinity is at least 75 percent.
 3. The method of claim 1 wherein the modifier is comprised of about 100 to 200 wppm Si and about 100 to 3000 wppm of an alkaline earth metal selected from Mg and Ca.
 4. The method of claim 3 wherein the modifier is comprised of about 100 to 200 wppm Si and about 200 to 1000 wppm of an alkaline-earth metal selected from Ca and Mg.
 5. The method of claim 1 wherein about about 0.01 to 2 wt. % rehnium is present.
 6. The method of claim 1 wherein about 0.01 to 2 wt. % tin is present.
 7. The method of claim 5 wherein about 0.1 to 0.7 wt. % rhenium is present.
 8. The method of claim 6 wherein about 0.1 to about 0.7 wt. % tin is present.
 9. The method of claim 3 wherein about 0.1 to 0.7 wt. % of each of platinum, iridium, and rhenium are present and the iridium is agglomerated to exhibit a crystallinity of substantially 100 percent. 